Peocess for producing melamine



Patented Aug. 18, 1953 PROCESS FOR PRODUCING MELAMINE Raymond A. Vingee, Stamford, Conn., assignor to Allied Chemical & Dye Corporation, New York, N. Y., a corporation of New York No Drawing. Original application May 9, 1947,

Divided and this application June 14, 1950, Serial No. 168,145

Serial No. 747,137.

4 Claims.

This invention relates to processes for the production of melamine and more particularly to processes for producing melamine from reactants comprising urea. This application is a division of my United States application Serial No. 747,137 filed May 9, 1947.

An object of the invention is to obtain melamine in good yields from urea or from reaction charges including urea as one reactant.

Another object is to obtain melamine from reactants comprising urea under relatively mild conditions of temperature, pressure and time of reaction.

A third object is to provide a catalyst for the formation of melamine from reactants comprising urea.

Other objects and advantages of my invention will appear hereinafter.

In the formation of melamine from urea or from reactants comprising urea, I have found that the reaction is catalyzed by addition of minor proportions of a compound which contains a sulfate anion. The materials which may be used to catalyze the reaction forming melamine, in accordance with my invention, include metaand pyrosulfuric acids and their salts as well as the ortho-compounds.

Some suitable conditions of temperature, pressure, etc. for heating urea to form melamine therefrom are known. I believe, however, I am the first to discover the catalytic effect on these reactions of the materials herein described. Accordingly, my invention is directed to processes employing those materials as catalysts added to urea which is heated under any conditions under which melamine is formed from the urea. Use of the catalysts to which my invention is directed promotes the reaction of urea to form melamine under milder conditions of temperature, pressure and reaction time than would be required in the absence of a catalyst. In its preferred aspects processes embodying my invention employ those milder conditions. Accordingly, without limiting the invention thereto, the preferred conditions for employing my catalysts will be described hereinafter.

The catalysts which are added to the reactants comprising urea in accordance with my invention are usually added in amounts of a few.

- mol percent of the reactants charged but larger amounts are also operative and with the more active catalysts small amounts of less than 1 mol percent of the charge show strong catalytic efiects. A practical maximum for the amount of added catalyst is about 3.0 mol Percent on the reactants charged. Suitably about 0.01 to 5 mol percent maybe used.

The catalysts of my invention include the organic salts of the above inorganic acids as well as the inorganic salts. For example, the guanidine salt of the catalytic acid may be formed in situ during the'reaction, g. by action of the reaction mixture on some or all of a catalytic acid, or on an ammonium salt or an anhydride thereof, added at the start; and the guanidine salt thus formed will function as a catalyst; or I may add at the start as a catalyst a guanidine salt of one of the above acids.

'It is not essential that the catalytic substances added to the charge in accordance with my invention should dissolve completely in the reaction mixture at any time during the reaction. I have obtained good catalytic effect from compounds which do not dissolve appreciably in the reaction mixture during the course of the reaction. However, if the substance added as a catalyst does not pass into solution, the catalytic substance should be added in a form to present a large surface area at which catalytic action may occur. I

Preferred catalysts are those which are soluble to the extent'of at least 1% by weight in water at 20 C. since these compounds have high activity and may be separated as water solutions from melamine.

:The following examples illustrate my invention, but it is not intended that these examples should limit the scope of the invention.

The apparatus used in Examples 1-2 below was a heavy'walled glass autoclave tube placed within a glass tube which was electrically heatedby a Nichrome winding and was insulated by an" outer glass tube. A thermocouple beside the autoclave tube was used for measuring the temperature.

The method of operation was to charge a weighed amount of urea and the substance added as a catalyst to the autoclave and heat the autoclave rapidly to reaction temperature. After the desired reaction period at reaction temperature the autoclave was allowed to cool and was then opened. The reaction time re' corded is the time at rea'ctiontemperature.

Melamine of about -100% purity was recovered from the products by driving off cammonium carbamate at C. to a condenser, digesting the residue, in a quantity of hot water moderatelyin excess of that required to dissolve a like amount of melamine, filtering off the hot water-insoluble portion (mostly am- 3 melide plus ammeline) and crystallizing melamine from the filtrate by cooling. Melamine Was identified by crystal form, solubility properties, melting behavior, elementary analysis, and preparation and analysis of the oxalate and picrate.

Example 1.-.Adding to 6.6 grams of urea per 100 cc. of reaction space, 4.1 weight percent ammonium sulfate (corresponding to a mol ratio of ammonium sulfate to urea of 0.01911) and heating the urea in a sealed glass reactor at 350- 360 C. for 0.8 hour gave substantially a 43.5 percent yield of melamine recovered,:inmolxpercent of the input urea.

Under the same conditions .except that added catalysts were absent, no melamine was formed in 0.5 hour reaction time. A good yield of melamine may be obtained on heating for 0.5 hour in a glass reactor in absence of an added catalyst only under much increased pressure of gaseous urea decomposition products .as compared to the above (e. g., about 9000 :p. s. 'i.) vor at .considerably higher temperature than above (e. g. 400 C.).

Example 2.Magnesium sulfate added in an amount of 5 weight percent (4.1 mol percent) to about 13.8 grams of urea per 100 cc. of reaction space, heated at 350-360C. and about 2800p. s. i. led to a 40.6 mol percent yield of melamine on the input urea after heating 0.5 hour at reaction temperature.

I have found cyclic pyrolysis products of a lower degree of animation than melamine are formed during the pyrolysis of urea and are ultimately converted to melamine. For example, a mixture of ammelide and ammeline may be isolated, in yields which decrease as melamine increases during the heating period. Thus, although in the above examples urea is the original reactant, .instead of starting with urea one may start with a reaction mixture comprising urea and oxygen-containing cyclic products of urea pyrolysis, e. g., cyanuric acid, ammelide or ammeline; or one may :start with-urea and a compound such as cyanic acid from which one or more of the above condensation products are formed on heating. Under the reaction conditions described :herein .as suitable for treating urea in accordance with my invention, mixtures initially containing urea andan oxygen-containr ing cyclic product of 'ureapyrolysis as :the reactants may be pyrolyzed to melamine in accordance with my invention. About one mol of urea is consumed in converting each mol of hydroxyl radical in the above cyclic compounds to an amino radical.

It is not necessary that the reactants specifled for my process be charged as such to the reactor. They may insteadbe formed in situ from other reactants, and in this case their formation often will be only transitory. For example, cyanic acid and ammonia may-beemployed as reactants instead of urea, since .thesercompounds can react on heating to form urea or its .initial decomposition products. Biuret, which gives essentially the same initialdecomposition products on heating as does urea, may likewise replace urea in my process. Thus, I intend to include within the scope of the term reactants comprising urea those reactants such as cyanic acid plus ammonia, or biuret, which form urea (at least transitorily) on heating.

The foregoing examples illustrate'the use of various catalysts in carrying out my invention. Conditions which exert an important influence on the yield ofmelamine from urea are reac- '4 tion temperature, time of reaction, and pressure of ammonia and carbon dioxide in the latmosphere over the charge.

A temperature of about 300 C., I have found, is sumcient to obtain satisfactorily rapid and complete conversion of urea to melamine with gas pressures in the reactor within the ranges discussed below, when certain materials which catalyze the urea conversion reactions are present. But higher temperatures, 6. g. 350-450 C. are preferred. A particularly preferred operating temperature is about 350-360 C. When the temperature is too low in relation to the pressure and the heating time, the urea tends to form oxygen-containing cyclic products rather than melamine.

Besides being affected by reaction temperature, the yield of melamine obtained in the pyrolysis of urea is also influenced by the pressure of the gaseous urea decomposition products in the atmosphere over the charge. These prodnets .are chiefly ammonia and carbon dioxide (formed from urea as the pyrolysis proceeds in mol ratios varying from about 4:1 to about 1:1 of .NH3ICO2). When the reaction is carried out in a sealed vessel, the pressure of ammonia and carbon dioxide depends on the amount of reactant material introduced originally into the closed vessel, since this figure determines both the quantity of each gas ultimately formed and the available space in the gas phase. In the examples above I have specified the amount of reactant (urea) introduced in the vessel in terms of grams of urea charged-per cc. of space in the reaction vessel. I have found that with the other conditions constant, the yield of melamine reaches an optimum as the value for the ultimate pressure of the gaseous decomposition products of urea (ammonia and carbon dioxide) reached during the urea decomposition reaction increases.

At any given temperature, increasing pressures of NEH-CO2 favor the reaction Water, if present, can hydrolyze melamine. The reaction of ammonia and carbon dioxide forming water is favored thermodynamically as temperature decreases so that as the reaction mixture is cooled, a temperature will be reached, higher the higher the pressure of ammonia and carbon dioxide, at which the formation of water occurs to an appreciable extent. If the pressure of NH: and CO2 is high and such that the NHs and CO2 can combine appreciably in the condensed phase at temperatures of 200 C. and above, then hydrolysis of melamine by the water formed will be correspondingly rapid during cooling of the products, and will reduce the ultimate melamine yield.

Rapid cooling of the products is accordingly advantageous to avoid loss of melamine, whenever appreciable water is present. If the apparatus allows reducing the pressure of the gases formed before the products are cooled, the formation of water at elevated temperature by combination of NH3+CO2 may be prevented and the hydrolysis of melamine from this cause can then be practically eliminated. The same is true if the pressure of the gases formed is always low enough so that no combination in the condensed phase of NH3+CO2 occurs except at relatively low temperatures, say below about 200 C. On the other hand, when the ultimate pressure of ammonia and carbon dioxide developed in the reaction is too low, deammoniation of melamine to melam, etc., may occur and reduce the melamine yield.

Thus, the optimum pressure of ammonia and carbon dioxide will vary with the precise manner of conducting the reaction and the subsequent cooling of the product. The precise choice of pressure is not highly critical, but in general a pressure of about 1000-3000 pounds per square inch of NE and CO2 is preferred at the preferred temperature of about 350-360 C. In the presence of a catalyst, I have employed successfully a. pressure of NH3 plus CO2 as low as about 350 pounds per square inch at a reaction temperature of about 350 C.

The pressure of NH3+CO2 under which these gases combine at the temperature of reaction sets a maximum pressure of NH3+CO2 for the process. This pressure is higher, the higher the reaction temperature employed. At 350-400 C., it is of the order of 10,000 atmospheres. The practical upper limit of pressure of NH3+CO2 is that which the equipment will stand. An NH3+CO2 pressure as high as 10,000 p. s. i. I have found to give satisfactory results in the process of my invention. The minimum pressure giving satisfactory results appears to depend somewhat on temperature; thus a higher pressure, or loading density, is required for satisfactory yield of melamine at 300 C. than at 400 C. reaction temperature, other things being equal. The preferred minimum pressure for temperatures in the preferred range (above about 300 C.) is about 1,000 p. s. i. of ammonia and carbon dioxide.

In the usual manner of operating my invention I obtain the required pressure of gaseous'urea decomposition products (chiefly ammonia and carbon dioxide) by the formation of these gases from the reaction mixture as reaction proceeds. At the beginning of a batchwise reaction the pressure of the gaseous urea decomposition products is below the above prescribed values. However, it is not necessary that the ammonia and carbon dioxide pressure exceed a particular value throughout the reaction: the values discussed above are those which should eventually be reached during the course of the reaction in order to obtain good yields of melamine.

It is not essential that all the gases present be derived from the decomposition of the urea reactant. For example if desired, NI-Is or CO2 or both introduced into the reactor from an external source may be used in place of or in addition to the NH3 or CO2 or both formed by decomposition of the urea reactant to maintain the desired pressure over the charge. An inert gas may be present over the charge in addition to NH: and CO2.

Furthermore, the ratio of NH; to CO2 present over the charge need not be such ratios as may be formed by the decomposition of the urea reactants. Ammonia or carbon dioxide or both may be added from some other source or removed from the atmosphere over the charge so as to establish a different ratio of these gases present over the charge than would result from urea decomposition alone.

But preferably the ratio of NI-Ia to CO2 is maintained within the range of ratios normally resulting from the decomposition of the urea during the reaction. This range, I have found, is from about 421-121 mol ratio of NH31CO2, and when the urea decomposes to melamine, ammonia and carbon dioxide in theoretical yields the ratio of NHaICOz formed, I have found, is about 2:1.

This ratio of about 2:1 for NH31CO2 represents a particularly preferred ratio of these gases over the charge according to m invention. Even if added NH; or added CO2 or other added gas is present over the charge, the partial pressure of NH3 (present from any source) should preferably reach at least about 650 p. s. '1. during the reaction and the partial pressure of CO2 (present from any source) should preferably reach at least about 300 p. s. i. during the reaction. These figures correspond to the preferred minimum pressure of about 1,000 p. s. i. of the gaseous urea decomposition products obtained when the conversion of urea to melamine, ammonia and carbon dioxide approaches the theoretical.

The minimum time of heating to reach satisfactory conversion to melamine is influenced by temperature, pressure of NH3 and CO2, and presence or absence of catalysts.

For example, with temperatures in the lower region of the preferred range, e, g., about 300 C., and with a moderate pressure of about 5,000 p. s. i. eventually developed during a batch reaction in a stainless steel autoclave, the yield of melamine reaches approximately its maximum value after about six hours of heating the urea charge. But at 350 C., under conditions otherwise the same, the reaction goes virtually to completion after 0.5 hour heating. When a high pressure of the NI-Is and CO2 gaseous products (about 10,000 p. s. i.) is developed at reaction temperatures of about 350 C., the yield of melamine from urea reaches more than of its maximum value in about one minute at reaction temperature. The preferred conditions comprise a heating time of the order of fifteen minutes, in a chromenickel steel autoclave at about 350-360 C. under about 1000-3000 p. s. i. pressure of urea decomposition products.

The time of heating may far exceed the minimum necessary for satisfactory conversion without any great deleterious effect on the melamine yield. Thus, as long as the time is sufficient for substantial conversion of the reactants to melamine under the conditions of temperature and pressure used, the particular time of heating is not critical. For example, under conditions which give a maximum conversion to melamine in about 0.5 hour, the reactants may be heated for several hours instead of 0.5 hour without much changing the yield of melamine obtained.

Substantial conversion to melamine may be recognized by incipient liquefaction of the reaction mixture at a temperature of 350-360 C., or by any other desired test for the presence of melamine in the reaction mixture.

I claim:

1. A process of producing melamine which comprises heating in a pressure resistant vessel urea and ammonium sulfate in amounts up to and including about 10 mol percent of ammonium sulfate based on the urea taken and maintaining the thus heated materials at temperatures between about 300 C. and about 400 C. and under high pressure until substantial quantities of melamine are present in the reaction mixture, and recovering from said reaction mixture melamine thus produced.

2. A process of preparing melamine which comprises heating urea and ammonium sulfate in a pressure resistant vessel at a temperature about 350 C. under high pressure and recovering the thus produced melamine.

3. A process for the production of melamine which comprises heating in absence of substan- 7, tial amounts of water reactants comprising urea in aflreaction zone'to which is added amounts up to and including about 10 mol percent on the reactants of at leastone material-of the group consisting of ortho, pyro and meta sulfuric acid, their inorganic salts and their guanidine salts, and continuing to heat the reaction mixture, at a temperature within the range-of about 300 C.- 450 C and in contact withian atmosphere containing ammonia and carbon dioxide in which the :partial pressure'of ammonia and carbon dioxide reaches at least-about 1000 p. s. i. during the reaction, 'until at least a substantial portion 8v of-therreactionvzmixture converted to melamine. 4. A process as defined in claim '3 in which the materialadded to the reaction zone dissolves at reaction temperature in the reaction mixture and 5 in which urea is the principal reactant charged.

RAYMOND A. VINGEE.

References Cited in the file of this patent 10 UNITED STATES PATENTS Number Name Date 2566228 Mackay Aug. 28, 1951 

1. A PROCESS OF PRODUCING MELAMINE WHICH COMPRISES HEATING IN A PRESSURE RESISTANT VESSEL UREA AND AMMONIUM SULFATE IN AMOUNTS UP TO AND INCLUDING ABOUT 10 MOL PERCENT OF AMMONIUM SULFATE BASED ON THE UREA TAKEN AND MAINTAINING THE THUS HEATED MATERIALS AT TEMPERATURES BETWEEN ABOUT 300* C. AND ABOUT 400* C. AND UNDER HIGH PRESSURE UNTIL SUBSTANTIAL QUANTITIES OF MELAMINE ARE PRESENT IN THE REACTION MIXTURE, AND RECOVERING FROM SAID REACTION MIXTURE MELAMINE THUS PRODUCED. 